JP5514835B2 - Process for preparing a free-flowing powder comprising a deliquescent quaternary ammonium compound - Google Patents

Description

  The present invention is a free flow comprising at least 85 parts by weight, preferably at least 90 parts by weight, more preferably at least 95 parts by weight, based on dry weight, of at least one deliquescent quaternary ammonium compound. It relates to a process for preparing a powder. This free-flowing powder is obtained by drying an aqueous solution of a quaternary ammonium compound to obtain a solid product, followed by at least one powdered salt of a medium to long chain fatty acid having a polyvalent counter ion. Prepared by mixing the solid product in an amount of at least 0.1 parts by weight per 100 parts by weight of the quaternary ammonium compound.

  Quaternary ammonium compounds such as betaine are deliquescent compounds, that is, powdered substances that readily absorb moisture from the ambient atmosphere to such an extent that spontaneous melting occurs (eg, obtained in pure form by crystallization or drying). Often. The rate at which this process (from the dry phase to the liquid phase) occurs depends on the individual compounds, but the intermediate stage always agglomerates and presents a sticky powder, which is cumbersome. This often requires a carrier material to stabilize the product during use, thereby reducing the concentration of the active ingredient and making it difficult to manage product safety.

  For example, choline chloride is used on a large scale as a feed additive in the animal feed industry. Usually, vitamins and trace elements are added to animal feed as a premix in dry form. However, choline chloride is often produced as a 75% aqueous solution. Anhydrous samples obtained by crystallization will absorb moisture from ambient air very quickly and become stuck. For this reason, choline chloride is actually sold in the solid form for animal feed after being absorbed by silica as a carrier or finely chopped plant material. However, in such processes, the choline chloride content of such products is generally limited to 70%. In addition, when a finely chopped and less expensive plant material is used as a carrier, the exact chemical composition and contamination level of the plant carrier is actually the most important for food and feed safety. Are often difficult to manage.

  For example, US 4,775,540 discloses a process in which silica is used as a support. In this process, a relatively large amount of silica is added to the 70-80% choline chloride solution, which reduces the choline chloride concentration from 40-50% by weight. Since the injectability of the powder mixture obtained in this way is still insufficient, 0.05 to 0.4% by weight of magnesium stearate or calcium stearate is mixed. The resulting powder could be poured through a 5 mm orifice, and even through a 20 mm orifice after 24 hours in 75% relative humidity air. The disadvantage of this process is that the relatively large amount of silica is required, so that the resulting product has a very limited choline chloride content.

  Instead of adding silica to the choline chloride solution, it is also known to add sodium stearate. Such a process is disclosed in NL6704009. In this known process, 25 parts by weight of sodium stearate per 100 parts by weight of choline chloride is added to a 70% by weight choline chloride solution. In such a method, a suspension is obtained and then dried. According to NL 670409, the suspension can be dried by drum drying or spray drying. However, only examples of drum drying processes are shown. Due to the high content of solid sodium stearate particles suspended in the choline chloride solution, in practice this solution is not at all suitable for spray drying (eg 75% containing only 3.8% silica). (See, for example, US Pat. No. 6,177,124, which states that choline chloride solutions are already too viscous to be atomized in a spray dryer). Furthermore, it is clear from NL6704009 that if the suspension is spray-dried, a solid product is obtained, which will need to be ground to make a powder. NL6704009 states nothing about the stability of the dried powder and how to evaluate its free flow properties. In the case of spray-drying a choline chloride solution containing a stearate (a small amount of sodium stearate and calcium stearate) suspended in a solution from a comparative test (see Comparative Example 7) conducted by the present inventors. In practice, a very lumpy material is obtained, but even if this lumpy material is crushed, it cannot still be poured through a 6 mm orifice and the stability is slightly limited. It is clear. By further comparative testing (see Comparative Example 9d), when the suspension prepared with NL6707049 was dried and ground, the resulting dry product had some free-flow properties, but a 6 mm orifice It was shown that it did not flow naturally through. Furthermore, during a stability test in which a thin layer of the dried and ground product is maintained at 20 ° C. and a relative humidity of 75%, the product already sticks after 1 hour and water drops appear on the surface after 2 hours. It was. Finally, the product obtained by the process disclosed in NL6707049 is relatively expensive due to its low choline chloride content and the high amount of sodium stearate required.

  Processes capable of obtaining free-flowing powders with a high choline chloride content are disclosed in US6177124 and DE2209477. These patent publications disclose the use of hydrophobic silica as an additive in solid choline chloride to prevent liquefaction of choline chloride and maintain sufficient free flow properties to ensure ease of handling. ing. In such a process, choline chloride is obtained in the form of a solid containing up to 95% active ingredient by spray drying a water-soluble silica-choline chloride suspension. However, hydrophobic silica is very expensive and has a significant impact on the price of the final product.

US 5486363 discloses a process in which dry free-flowing choline chloride, again containing powder, is produced with the aid of hydrophobic silicic acid. Instead of mixing the hydrophobic silicic acid powder into the choline chloride solution, the powder is finely dispersed in a countercurrent air stream in a spray drying tower. A product with a high content of choline chloride (containing only 2.7% by weight of SiO ₂ ) was obtained. However, in order to obtain a sufficiently dry powder, a two-stage drying or height (20-30 m) spray dryer is required. US 5486363 also suggests using much cheaper fatty acid salts instead of hydrophobic silica. However, experimental data is not shown. The inventors have used a flow of air in a drying chamber of a spray drying tower to add calcium stearate powder in an amount such that the dried choline chloride contains 2.5% by weight calcium stearate (Comparative Example 8a). To see). This process disclosed in US Pat. No. 5,486,363 is clearly much more expensive because the product obtained was not free flowing, even when 1% calcium stearate was not mixed into the dried product. It was clear that it was effective only with the help of hydrophobic silica.

  DD84552 discloses a process for preparing a solid choline chloride product with a high choline chloride content, which uses cheaper fatty acid salts. In this known process, the choline chloride solution is dried and a vacuum is utilized to avoid or limit moisture absorption. Thereafter 0.5 to 10 parts, preferably 2 to 5 parts of calcium stearate or magnesium stearate are mixed with the dried choline chloride. The problem with this known process is that the dried choline chloride is very hygroscopic and starts to adhere immediately to the cooler part of the drying / cooling device (see Comparative Example 6). Therefore, this drying process can be performed only for a limited time before the dryer needs to be serviced. Furthermore, although DD84552 describes the production of a free-flowing product, it is clear that the flowability still needs to be improved. Indeed, from the comparative example 8a already described above, when the choline chloride solution is spray dried and the dried choline chloride is mixed with 1% calcium stearate, an additional about 2.5% is added during the spray drying stage. It can be seen that despite the fact that the calcium stearate was added to the choline chloride, the resulting product still did not flow through the 6 mm orifice.

  The object of the present invention is such that the resulting powder contains a relatively high content of quaternary ammonium compounds (no more than 6 mm in diameter) without the need to use expensive hydrophobic silica or large amounts of other additives or carriers. It is to provide a new process whereby a free-flowing powder (which can flow through an orifice) can be produced from a solution of deliquescent quaternary ammonium compounds, in particular a choline chloride solution. This new process should also prevent deliquescent quaternary ammonium compounds from sticking to the dryer, especially when using a spray dryer.

  To achieve the above objective, the process according to the present invention is based on the water solubility of at least one medium to long chain fatty acid having a monovalent counterion before drying an aqueous solution of a deliquescent quaternary ammonium compound. A salt is added, and at least 0.1 part by weight of the water-soluble salt per 100 parts by weight of the quaternary ammonium compound is dissolved in the aqueous solution.

  After drying the aqueous solution, a solid product is obtained, in which at least 0.1 part by weight per 100 parts by weight of the quaternary ammonium compound is in the form of a powder of medium to long chain fatty acids having at least one polyvalent counter ion. Of salt is mixed.

  The inventors have first dissolved an amount of a water-soluble fatty acid salt having a monovalent counterion in an aqueous solution, dried the aqueous solution into a solid product, and then added a large amount to the resulting dried product. It has been discovered that when a powdered salt of a fatty acid having a valence counter ion is mixed, a free-flowing powder having better free-flowing properties can be obtained with a smaller amount of fatty acid salt. In this regard, it should be noted that when the patent specification states that the inventive powder is free-flowing, this means that the powder flows by gravity through a round orifice with a diameter of only 6 mm. .

  It has been found that there is a synergistic effect between the fatty acid salt dissolved in the aqueous solution and the fatty acid salt mixed with the dried product, especially on the free flow properties of the resulting powder. In order to achieve such a synergistic effect, it seemed essential that a minimum amount of water-soluble fatty acid salt was actually dissolved in the aqueous solution. When a fatty acid salt that is insoluble in water, such as calcium stearate, is added to the aqueous solution, the dried solid product is then mixed with a powdered fatty acid salt (specifically calcium stearate) to obtain a free flowing powder. I couldn't. However, when the aqueous solution contained only a relatively small amount of dissolved fatty acid salt, the free flow characteristics of the resulting powder were significantly improved by subsequently mixing the powdered fatty acid salt into the dried powder. The reason for this synergistic effect is not clear, but a possible hypothesis is that the fatty acid chains of the dissolved fatty acid salt migrate between the gas-liquid surfaces and concentrate on the surface of the dry particles (in this case it is very thin It may also form a film), where it interacts with the powdered fatty acid salt to increase the flowability of the powder. In contrast, if the fatty acid salt particles are not dissolved in the aqueous solution but are only suspended, the fatty acid salt particles remain more in the product core and form a film on the surface of the powder particles. It cannot be formed.

  In a preferred embodiment of the process according to the invention, the aqueous solution is heated to a temperature above 50 ° C., preferably above 60 ° C., more preferably above 75 ° C. in order to dissolve the water-soluble salt in the aqueous solution.

  Water-soluble fatty acid salts have only limited solubility in water. By heating the aqueous solution, more fatty acid salts can be dissolved in water. This is particularly important in the case of aqueous solutions containing higher amounts of deliquescent quaternary ammonium compounds. This is because the solubility of the fatty acid salt in the above solution is even lower. In contrast, in the process disclosed in NL 670409, an aqueous solution containing 70% choline chloride is not heated, and as described herein, suspension is achieved when sodium stearate is added to the aqueous solution. In this case, despite the large amount of sodium stearate added to the aqueous solution, there is no or almost no sodium stearate dissolved therein.

  The invention also relates to a free-flowing powder obtained by the process according to the invention, in particular it remains free-flowing even when stored for 3 hours at 20 ° C. and 75% relative air humidity as a thin layer of about 3 mm. Relates to free-flowing powder.

  The present invention further includes vitamins, minerals, antioxidants, antibacterial agents, anthelmintic agents, microbial supplements, oligosaccharides, enzymes, amino acids, acidifying agents, flavoring agents, foul odor preventing agents, pellet binders, fluidizing agents, fats, It relates to a feed additive mixture comprising a free-flowing powder according to the invention mixed with at least one additional powder selected from the group consisting of carotenoids and meat modifiers.

  Further details and advantages of the present invention will become apparent from the following more detailed description of the process, free-flowing powder and feed additive mixture according to the present invention.

  The present invention comprises at least 85 parts by weight, preferably at least 90 parts by weight, more preferably still at least 95 parts by weight, based on dry weight, of at least one deliquescent quaternary ammonium compound per 100 parts by weight of powder. It relates to a process for preparing flowable powders.

  The term deliquescent compound refers to a compound that absorbs moisture from the ambient atmosphere to the extent that melting occurs before the equilibrium water content is reached (at a temperature of 20 ° C. and a relative humidity of 75%). Quaternary ammonium compounds are organic molecules that bind to four carbon atoms and thus contain at least one nitrogen atom that is positively charged. As counter ions, organic anions as well as inorganic anions can occur. Examples include, but are not limited to, halides, carboxylates, carbonates, sulfates or hydroxides. Betaine is known as a special kind of quaternary ammonium compound that has both a positive charge (ammonium nitrogen atom) and a negative charge (oxygen atom of carboxylic acid) in the same molecule. Examples of deliquescent quaternary ammonium compounds such as betaine that are advantageously treated under the conditions of the present invention include choline species (choline chloride, choline bromide, choline hydroxide, choline carboxylate, choline carbonate) Glycine betaine, tetramethylammonium chloride and tetramethylammonium bromide, D, L-carnitine and the like.

  As already mentioned above, the term “free-flowing powder” refers to a powder that can flow by gravity through a round orifice with a diameter of only 6 mm.

  In order to prepare a free flowing powder, an aqueous solution of a deliquescent quaternary ammonium salt is used. This solution is dried to make a dry solid product. In order to reduce the drying capacity required for this drying step, the aqueous solution preferably contains more than 50% by weight of quaternary ammonium salt, preferably more than 60% by weight, more preferably more than 70% by weight.

  The drying stage can be performed in various ways that can be divided into two main types: contact drying and convection drying (with dry air). Contact drying techniques include hot plate drying and drum drying, while convective drying techniques include fluidized bed drying, airflow drying and spray drying including spray granulation and spray agglomeration.

  An essential feature of the process of the present invention is that before drying the aqueous solution, at least one water-soluble salt of medium to long chain fatty acids having a monovalent counterion is added, and the deliquescent quaternary ammonium compound 100 is added. At least 0.1 parts by weight of this water-soluble salt per part by weight is actually dissolved in this aqueous solution. The amount of water-soluble salt added to the aqueous solution is preferably less than 10 parts by weight, more preferably less than 5 parts by weight, and most preferably less than 3 parts by weight per 100 parts by weight of the quaternary ammonium compound. In practice, water-soluble salts have only limited solubility in water, so if too much is added, that part will remain in the suspension. This increases the viscosity of the aqueous solution, which can cause problems especially when the solution is dried by techniques that require the solution to be atomized. Furthermore, the portion of the water-soluble salt that will remain suspended in the solution does not contribute substantially to its free-flowing properties and reduces the concentration of the final product ammonium compound. Thus, preferably, more than 20%, more preferably more than 50%, and most preferably more than 75% of the water-soluble salts added to the aqueous solution are dissolved in the aqueous solution before the solution is dried.

  It is preferred that the aqueous solution is heated to a temperature in particular above 50 ° C., preferably above 60 ° C., more preferably above 75 ° C. so that more water-soluble salt can be dissolved. Preferably, at least 0.2 parts by weight, more preferably at least 0.3 parts by weight, and most preferably at least 0.4 parts by weight of the water-soluble salt is dissolved in an aqueous solution per 100 parts of the quaternary ammonium compound. Yes.

  The medium to long chain fatty acid of the water-soluble salt dissolved in the aqueous solution has a chain length of 7 to 23 carbon atoms, preferably 8 to 18 carbon atoms. The water-soluble salt is preferably an alkali metal salt, particularly a lithium, sodium or potassium salt, but may also be an ammonium salt. Suitable fatty acids include natural or odd fatty acids such as caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, arachidic acid, behenic acid, palmitoleic acid, oleic acid, linoleic acid and linolenic acid. Synthetic fatty acids or branched fatty acids having a chain length between 7 and 23 carbon atoms. Mixtures of fatty acid salts may also be used. Water soluble salts can be added to an aqueous solution by adding the salt to the aqueous solution or by forming a salt in the aqueous solution, for example by adding precursor molecules such as the parent fatty acid and the corresponding alkali metal hydroxide. it can. Other additives such as glycerol, silica, carbonate, polyvinyl alcohol, colorants, etc. may be added to the resulting liquid to improve certain properties of the final product.

  The resulting liquid is very suitable for drying. Drying can be done by various means as already described herein above. Hot plate drying and spray drying appeared to be particularly suitable. Using hot plate drying often results in a glass-like material that can be easily handled and that can be easily fined to the desired final form. When spray drying was used, particles between 20 and 200 μm could easily be obtained in a normal spray drying facility using a nozzle or a rotating disc sprayer. Larger by spray granulation (dry particles are recycled to the drying chamber with fresh aqueous solution until desired size) or spray agglomeration (adhesive applied to dry particles to form agglomerates) Particles can be obtained. In contrast to US 5486363, a dry product (having a water content of less than 1%, preferably less than 0.5%) can be obtained in one stage without the need to use a long and thin special spray dryer. .

  If water-soluble fatty acid salts, particularly alkali metal fatty acid salts, are not used, the problem of sticking and clumping during drying is often observed. In addition, the product is difficult to handle because it rapidly absorbs moisture during cooling after the drying stage. However, it is thought that all operational problems can be avoided by adding a water-soluble fatty acid salt to the liquid feed. In addition, the resulting product was already quite free-flowing, but the stability under ambient conditions was still poor.

  In accordance with the present invention, both free-flowing behavior and stability under ambient conditions are obtained by further mixing a powdered salt of medium to long chain fatty acids with at least one multivalent counterion into the solid product. Is greatly improved. This solid product is obtained after drying of the aqueous solution and preferably has a water content of less than 10% by weight, preferably less than 5% by weight, more preferably less than 3% by weight.

  The medium to long fatty acid fatty acid in the form of powdered fatty acid has a chain length of 7 to 23 carbon atoms, preferably 8 to 18 carbon atoms. The powdered salt can be other divalent metal ions such as zinc, copper or cobalt, or trivalent metal ions such as iron, but is preferably an alkaline earth metal salt, particularly a magnesium or calcium salt. Suitable fatty acids are again natural or odd fatty acids such as caprylic acid, capric acid, lauric acid, myristic acid, palmitic acid, stearic acid, arachidic acid, behenic acid, palmitoleic acid, oleic acid, linoleic acid and linolenic acid Or a branched fatty acid having a chain length between 7 and 23 carbon atoms. Mixtures of fatty acid salts may also be used. In addition, other additives known to those skilled in the art, such as silica powder, especially fumed silica or fused silica, sulfates, carbonates, colorants, etc., to obtain the specific attributes of the final product as desired. May be added simultaneously. Advantageously, 0.1 to 1.0 part by weight, preferably 0.2 to 0.5 part by weight of silica powder per 100 parts by weight of the quaternary ammonium compound is mixed with the dried solid product. In such a way, it would be possible to avoid packing the free-flowing powder into a closed container (bag) in which it is stored.

  The powdered fatty acid salt must be mixed with the dried solid product in powder form. Powder mixing can be done by various techniques that meet the results: fluid bed mixer, paddle mixer, tumbler mixer, high shear mixer, and the like. The powdered salt is mixed with the dried solid product in an amount of at least 0.1 parts by weight per 100 parts by weight of the quaternary ammonium compound. Preferably, the powdered salt is in an amount of at least 0.5 parts by weight, more preferably at least 1.0 parts by weight, most preferably at least 1.5 parts by weight per 100 parts by weight of the deliquescent quaternary ammonium salt. Mixed with the dry solid product in parts. In order to keep the content of the quaternary ammonium compound in the final product as high as possible, the powdered salt is preferably less than 10 parts by weight per 100 parts by weight of the deliquescent quaternary ammonium salt, more preferably It is added in an amount of less than 6 parts by weight, most preferably less than 4 parts by weight.

  Preferably the free-flowing powder has an average particle size of more than 20 μm, preferably more than 50 μm, more preferably more than 100 μm, but less than 1000 μm, preferably less than 800 μm, more preferably less than 600 μm. The average particle size is a volume average, i.e. 50% by volume of particles have a size smaller than the average particle size, and 50% by volume has a larger particle size. The advantage of a large particle size is that the same stability and free flow properties can be achieved with less powdered fatty acid salts.

  Products obtained using an appropriate amount of water-soluble fatty acid salt (s) in the drying stage or using an appropriate amount of powdered fatty acid salt (s) during the powder mixing stage are: Excellent free flow and stability under ambient conditions. On the other hand, satisfactory results were obtained only by combining these two salts as described above: a water-soluble fatty acid salt dissolved in the feed liquid in the drying stage and dried in the second stage. Powdered metal salt mixed in form. If the fatty acid salt was omitted in one of the two stages, the product no longer exhibited the desired properties. Simply changing the order of the addition of the two fatty acid salts, so adding the polyvalent metal fatty acid salt in the drying stage and adding the monovalent metal fatty acid salt in the mixing stage will improve the quality of the final product. There was a disadvantage.

  The free-flowing powder obtained by the process according to the invention preferably comprises at least 80% by weight, more preferably at least 90% by weight and most preferably at least 95% by weight quaternary ammonium salts. Since this powder is free-flowing, it flows through a round orifice with a diameter of only 6 mm by gravity. Furthermore, since this free-flowing powder is stable, it preferably remains free-flowing even if maintained as a thin layer having a thickness of about 3 mm for 3 hours at 20 ° C. and 75% relative air humidity. Yes. Since this free-flowing powder is stored in a sealed container, particularly a sealed bag, it can be stored for a very long time without losing its free-flowing properties.

Free-flowing powders can be used in particular to prepare feed additive mixtures. This feed additive mixture is obtained by mixing a free-flowing powder with other powders to form a so-called premix. Other powders include vitamins, minerals, antioxidants, antibacterials, anthelmintics, microbial supplements, oligosaccharides, enzymes, amino acids, acidifying agents, flavoring agents, anti-odour agents, pellet binders, fluidizing agents, fats , Carotenoids and meat modifiers may be included. The feed additive mixture usually contains between 1 and 15% by weight of the free flowing powder of the invention. The other powders mentioned above are described in more detail below:
-National research Council (NRC), 1993, Nutrient Requirements of Fish, pages 3-37-National research Council (NRC), 1994, Neutral Requirements of PoI, 3-N (NRC), 1998, Nutrient Requirements of Swin, Tenth Revised Edition, pages 74-99, various publications cited as examples of these publications, particularly additives, are hereby incorporated by reference. Shall.

  The flowability of the powder was evaluated by adding 200 ml to the funnel and measuring the time taken to flow out of the opening (diameter 6 mm). Dry fine sand was used as a reference (33 seconds).

  The stability of the product was observed by spreading 1 g of choline chloride in a thin layer of 2 mm on an aluminum plate and storing it in a climate chamber at 20 ° C. and 75% relative humidity. This test should represent on a short time scale how large quantities of product stored in an open bag will behave over a few days. When the same test was used on 60% choline chloride contained in a commercial corn cobs (plant carrier) as a reference, the product started to stick after 90 minutes.

(Example 1)
A mixture of 15 kg of 55% aqueous choline chloride and 125 g of sodium stearate was heated to 60 ° C. This solution was supplied to a spray dryer (diameter 2 m, height 4.5 m, inflowing air 160 ° C.) through a jet nozzle. The dried product was collected at the bottom of the cyclone. This included 0.6% water and 1.5% sodium stearate. The rest was choline chloride. No deposits could be observed in the drying chamber, cyclone or rotary valve. The product was allowed to cool and then 500 g was added to a lab scale Lodige mixer with 10 grams of calcium stearate and 1 g of silica, Sipernat® 22S. After mixing for 15 minutes, a fine, free-flowing powder without lumps was obtained.
* Particle size d50 = 70 μm (volume average)
* Fluidity = 29 seconds * Stability: No lumps or water droplets could be observed within 5 hours

(Example 2)
A mixture of 15 kg of 70% aqueous choline chloride, 80 g sodium palmitate and 80 g sodium stearate was heated to 95 ° C. This solution was supplied to a spray dryer (diameter: 2 m, height: 4.5 m, inflowing air: 200 ° C.) by a rotary disk type spraying device. With a separate air stream, silica, Sipernat® 22S was sprayed directly into the dryer at a rate corresponding to 0.2% with respect to the dry product. The dried product was collected at the bottom of the cyclone and continuously mixed with 2% calcium stearate in a paddle mixer. The average residence time in the mixer was approximately 8 minutes. The obtained powder was free from lumps and exhibited good free flow.
* Particle size d50 = 90 μm
* Fluidity = 35 seconds * Stability: No lumps could be observed. After 3 hours, only water droplets could be observed on the surface.

(Example 3)
A mixture of 15 kg of 55% aqueous choline chloride, 30 g sodium palmitate and 90 g sodium oleate was heated to 60 ° C. This solution was supplied to a spray dryer (diameter 2 m, height 4.5 m, inflowing air 160 ° C.) through a jet nozzle. The dried product was collected at the bottom of the cyclone. This contained 0.7% water and 97.9% choline chloride. No deposits could be observed in the drying chamber, cyclone or rotary valve. The product was allowed to cool and then 500 g was added to a lab scale Lodige mixer with 15 grams of calcium stearate and 2 g of CaCO 3. After mixing for 15 minutes, a fine, free-flowing powder without lumps was obtained.
* Particle size d50 = 72 μm
* Fluidity = 30 seconds * Stability: No lumps or water droplets could be observed within 5 hours

(Example 4)
A mixture of 2 kg of 75% aqueous choline chloride, 20 g glycerol and 20 g sodium stearate was heated to 95 ° C. The liquid was then poured into a thin layer on a hot ceramic plate at 240 ° C. Solidification occurred very rapidly and a glass-like layer was formed on the plate. After 2 minutes, the plate was cooled to 40 ° C., and dried choline was scraped from the surface to obtain coarse particles. 500 g of this material was ground and sieved and then mixed with 10 g of powdered calcium stearate and 1 g of silica, Sipernat® 22S in a lab scale Lodige mixer. The water content of the obtained powder was 1.1%.
* Fluidity = 30 seconds * Stability: No lumps or water droplets could be observed within 5 hours

(Example 5)
A mixture of 4.2 kg of 60% aqueous glycine betaine solution, 6.5 g sodium palmitate and 6.5 g sodium stearate was heated to 50 ° C. This solution was supplied to a spray dryer (diameter 2 m, height 4.5 m, inflowing air 160 ° C.) through a jet nozzle. The dried product was collected at the bottom of the cyclone. This contained 0.5% water and 98.9% glycine betaine. No deposits could be observed in the drying chamber, cyclone or rotary valve. The product was allowed to cool, after which 500 g was added to a laboratory scale Lodige mixer with 7.5 grams of calcium palmitate and 7.5 grams of calcium stearate. After mixing for 15 minutes, a fine, free-flowing powder without lumps was obtained.
* Particle size d50 = 74 μm
* Fluidity = 31 seconds * Stability: No lumps or water droplets could be observed within 24 hours

(Comparative Example 6)
A 75% choline chloride aqueous solution was supplied to a spray dryer (diameter 2 m, inflowing air 165 ° C.). The dried product was collected at the bottom of the cyclone. This contained 1.2% water. This product came out mainly as a mass of material. This was difficult to handle in subsequent process steps due to increased viscosity. In addition, after a short drying operation, some deposits could be observed on the cyclone and rotary valve.
* Particle size: No measurement * Fluidity: No measurement (lumps)
* Stability: Water drop on the surface after 5 minutes; complete melting after 30 minutes

(Comparative Example 7)
To 60 kg of 55% choline chloride aqueous solution at 60 ° C., 120 g of sodium stearate and 165 g of calcium stearate were added. After mixing for 30 minutes with an ultraturrax mixer, a stable dispersion was obtained for at least a few hours. This dispersion was spray dried as illustrated in Example 1. The product recovered at the bottom of the cyclone was very agglomerated, so the particle size and flowability could not be measured. After milling of the product, the resulting powder still showed fluidity that was too low for measurement. Furthermore, the product had clearly visible water droplets already 90 minutes after the stability test. This example shows that the order in which the alkali metal and alkaline earth metal fatty acid salts are added is important.

(Comparative Example 8a)
A 75% choline chloride aqueous solution was supplied to a spray dryer (diameter: 2 m, height: 4.5 m, inflowing air: 160 ° C.) using a rotary disk spray device. Alkali metal fatty acid salts were not added to the feed. Instead, solid calcium stearate was added directly to the drying chamber by a stream of air. This calcium stream was added to contain 2.5% in the final product. The product was collected at the bottom of the cyclone and allowed to cool. This product tended to become stone upon cooling.

500 g of product was then mixed with 5 g of calcium stearate for 15 minutes in a lab scale Lodige mixer. The water content of the final product was 0.5%.
* Particle size d50 = 50 μm
* Fluidity: Not flowing * Stability: No water droplets could be observed within 5 hours

(Comparative Example 8b)
500 g of the powder obtained after drying Comparative Example 8a was mixed with 7.5 g of sodium stearate for 15 minutes in a lab-scale Lodige mixer. The water content of the final product was 0.5%.
* Particle size d50 = 50 μm
* Fluidity: Not flowing * Stability: No water droplets could be observed within 5 hours

  Both Comparative Examples 8a and 8b show that the alkali metal fatty acid salt must be present in a dissolved state prior to drying.

(Example 9)
A 75% aqueous choline chloride solution, heated to a temperature of 80 ° C. and containing 0.5% sodium stearate / sodium palmitate (50:50) based on the dry substance, was fed to the spray granulator through a nozzle. The cyclone collects fine particles from the outflow air at the top of the dryer and then recirculates it to the bottom of the dryer to maintain the bed, spraying the liquid onto a stable bed of choline chloride particles. The material was dried in a hot air stream (inlet air temperature 165 ° C.). Collect heavy particles (granules) from the floor with a particle sorter.

  The granules themselves obtained in the first part were tested in a climate chamber (Comparative Example 9a). In the dry mixing stage, the second part was further treated with 2% sodium stearate in solid form (Comparative Example 9b). In the dry mix stage, the third part was treated with 2% calcium stearate in solid form (Example 9c).

  A fourth sample (Comparative Example 9d) was prepared according to NL 670409 Example 1 as follows: A 70% aqueous solution of choline chloride in sodium stearate (20% based on dry matter) suspension was stirred vigorously at room temperature. It was produced by. The resulting milky liquid was dried on a hot plate. The resulting solid was ground before being added to the climate chamber along with the other three samples.

  When kept dry, Samples 1, 2 and 3 were free flowing. Sample 4 did not flow naturally through the funnel.

  The following main differences could be further observed in the stability test: Samples 1, 2 and 4 started to stick together after 1 hour and water drops were clearly seen on the surface after 2 hours, It was still evaluated as free flowing after 5 hours.

Claims (14)

A process for preparing a free-flowing powder comprising at least 85 parts by weight of at least one deliquescent quaternary ammonium compound per 100 parts by weight of free-flowing powder, based on dry weight, The free-flowing powder is obtained by drying an aqueous solution of the quaternary ammonium compound until it becomes a solid product, and then adding at least one powdered salt of a medium to long chain fatty acid having a polyvalent counter ion. Prepared by mixing into the solid product in an amount of at least 0.1 parts by weight per 100 parts by weight of a quaternary ammonium compound and having at least one monovalent counterion before drying the aqueous solution. A water-soluble salt of a long-chain fatty acid is added from the chain, and at least 0.1 parts by weight of the water-soluble salt is added to the aqueous solution per 100 parts by weight of the quaternary ammonium compound. Characterized in that it is dissolved, the process. The process of claim 1, wherein at least 0.2 parts by weight of the water-soluble salt per 100 parts of the quaternary ammonium compound is dissolved in the aqueous solution. Wherein in order to water-soluble salt is dissolved in the aqueous solution, wherein the aqueous solution, characterized in that it is heated to the 50 ° C. than the temperature A process according to claim 1 or 2. 4. Process according to any one of the preceding claims, characterized in that more than 20% of the water-soluble salt added to the aqueous solution is dissolved before the solution is dried. Wherein the water-soluble salts of quaternary ammonium compounds per 100 parts by weight 10 parts by weight less than, characterized in that added to the aqueous solution, the process according to any one of claims 1 to 4. 6. Process according to any one of the preceding claims, characterized in that the aqueous solution to which the water-soluble salt is added comprises more than 50% by weight of the quaternary ammonium salt. 7. At least 0.5 part by weight of the powdery salt per 100 parts by weight of the quaternary ammonium compound is mixed with the solid product according to any one of claims 1-6. The process described. The powdered salt of 10 parts by weight less than per the 100 parts of ammonium compounds No. 4, characterized in that it is mixed with the solid product, according to any one of claims 1 to 7 process.   9. Process according to any one of claims 1 to 8, characterized in that the quaternary ammonium compound comprises choline chloride. Wherein the aqueous solution, atomizing said solution into small droplets and dried by drying these droplets generates the dried particles, the aqueous solution, the gas flow drying, fluidized bed drying or spray granulation and 10. Process according to any one of claims 1 to 9, characterized in that it is dried by spray drying also including spray agglomeration.   Free-flowing powder obtainable by the process according to any one of claims 1 to 10. It is a 20μm greater, and having an average particle diameter of 1000μm less than, free-flowing powder according to claim 11.   The free-flowing powder according to claim 11 or 12, wherein the free-flowing powder remains as a thin layer of about 3 mm when stored for 3 hours at a temperature of 20 ° C and a relative air humidity of 75%.   Vitamins, minerals, antioxidants, antibacterial agents, anthelmintics, microbial supplements, oligosaccharides, enzymes, amino acids, acidifying agents, flavoring agents, foul odor preventing agents, pellet binders, fluidizing agents, fats, carotenoids and meat modification A feed additive mixture comprising a free-flowing powder according to any one of claims 11 to 13 mixed with at least one additional powder selected from the group consisting of agents.